KR100228075B1 - A separation membrane module and a waste water disposal method using the same - Google Patents

Abstract

A plurality of hollow fiber membranes 3 formed in a U-shape and both ends of the hollow fiber membranes 3 are fixed, and an upper end portion 2 for pulling permeate from the hollow fiber membranes 3 and the U-shaped The membrane module for wastewater treatment including a ring-shaped membrane support part 4 in which the central portion of the hollow fiber membrane 3 is hung is resistant to contamination of the membrane even at a high concentration of suspended solids among the membrane modules capable of solid-liquid separation. In addition to preventing contamination of the membrane and simultaneously supplying air in the microbial reactor, economical and workability is excellent, and system configuration is easy.

Description

Membrane Module and Wastewater Treatment Method Using the Same

[Industrial use]

The present invention relates to a membrane module, and more particularly, as a membrane module for improving the removal efficiency of organic substances and suspended solids by combining with biological wastewater treatment process, to prevent entanglement and contamination of the membrane used and organic matter decomposition of activated sludge. The present invention relates to a wastewater treatment apparatus including a membrane module and a membrane module capable of simultaneously supplying air necessary for a gas.

[Prior art]

As the necessity of efficient use of water resources is raised and the water quality standards are strengthened, it is difficult for the existing biological sewage and wastewater treatment process to secure stable water quality continuously. Therefore, it is necessary to combine physical and chemical treatment processes with existing biological treatment processes. Complex sewage and wastewater treatment processes have been developed.

One of the above wastewater and wastewater treatment processes is a process of combining a membrane process with a biological treatment process. For example, treated water is subjected to a biological treatment process again using a membrane separation device to suspend solids of treated water. : The process of reducing SS) is mentioned.

50배 정도의 유입수량이 필요하고 이 유입수는 펌프로 가압송수해야 하기 때문에 높은 동력비가 소요된다. 또한 막 장치의 점검 및 교환작업이 복잡하고 분리막을 설치해야 하는 공간이 별도로 필요하며, 폐수 중의 이물질들과 생물학적 처리공정내의 부유고형물들에 의한 막의 폐색이 쉽게 발생하여 막을 세정하기 위한 정기적인 약품세정이 필요하고 막의 수명이 짧아지는 문제가 있다.Although sewage and wastewater treatment technology using membrane technology such as reverse osmosis (RO), ultrafiltration (UF) and microfiltration (MF) has been used for a long time, Since it was developed for the purpose of recovering fires, it has a disadvantage of relatively high facility and maintenance costs. Especially, when the membrane process is applied to sewage and wastewater treatment, the membrane permeability due to the cake layer deposited on the membrane surface In order to prevent this fall, the cross-filtration method which filters while wash | cleaning by the discharging force by flow water was used. However, this method uses 40 per

Since 50 times the amount of inflow is required and this inflow has to be pressurized by pump, high power cost is required. In addition, the inspection and replacement of the membrane device is complicated, and a separate space for installing the membrane is required, and the membrane is periodically blocked by foreign substances in the wastewater and suspended solids in the biological treatment process. This is necessary and there is a problem that the life of the membrane is shortened.

In order to solve this problem, a technique of operating a membrane by directly depositing it in a biological treatment process has been attempted. It can be said that it is an important problem to prevent the contamination of the membrane from the suspended solids at a high concentration and to secure a continuous permeate flow rate. However, hydrophobic organic polymer membranes such as polysulfone, polyethylene, and polypropylene, which are mainly applied, are showing limitations for performance due to contamination by solid materials and organic materials. In order to solve this problem, a method of injecting air from the lower part of the membrane or shaking the membrane using an agitator to remove the solid and organic substances attached to the polymer membrane has been introduced. There is a problem that the device is complicated to configure, which makes the operation method difficult and the configuration of a compact device is difficult.

The present invention is to solve the problems of the prior art as described above, an object of the present invention is to reduce the number of inspection and replacement operations of the membrane device, has a structure resistant to membrane fouling even at high concentrations of suspended solids concentration and entanglement of the membrane In order to provide a membrane module of the economical and workability and easy system configuration that can be combined with the air supply in the microbial reaction tank with pollution prevention, easy to clean and oxygen supply unit.

Figure 1 (a) is a schematic longitudinal cross-sectional view of a conventional membrane module for wastewater treatment.

Figure 1 (b) is a schematic longitudinal cross-sectional view of the membrane module for wastewater treatment according to an embodiment of the present invention.

Figure 2 is a schematic cross-sectional view of the membrane support of the membrane module for wastewater treatment according to an embodiment of the present invention.

Figure 3 is a schematic longitudinal cross-sectional view of the fluid flow in the membrane and the module during the permeation and backwashing process according to an embodiment of the present invention.

4 (a) and 4 (b) is a process chart showing a washing process according to an embodiment of the present invention.

5 (a) and 5 (b) is a process chart showing the washing and backwashing process according to an embodiment of the present invention.

* Explanation of symbols for main parts of the drawings

1: treatment water discharge and backwash air inlet 2: membrane module upper part

3: hollow fiber separator 4: separator support

5: Internal diffuser device for washing membrane 6: Distributing membrane and preventing tangling

[Means for solving the problem]

In order to achieve the above object, the present invention has a plurality of hollow fiber membranes 3 formed in a U-shape and both ends of the hollow fiber membranes 3 are fixed, and the permeate is extracted from the hollow fiber membranes 3. Provided is a membrane module including a ring-shaped separator support portion 4, the upper end portion and the central portion of the U-shaped hollow fiber membrane 3 is hung.

It is preferable to further include an internal air dispersing device (5) located in the center of the separation membrane module for supplying air for washing the separation membrane.

1

이며 유효막면적이 1

100㎡/module인 것이 바람직하다.It is preferable that the separator support 4 has a plurality of air supply holes for supplying oxygen or air, and the effective pore size of the air supply holes is 0.005.

One

The effective film area is 1

It is preferable that it is 100 m <2> / module.

In addition, the membrane support 4 preferably has 1 to 16 anti-tangling projections.

The shape of the membrane module is preferably selected from the group consisting of cylindrical, square and conical.

In addition, in the present invention, both ends of the plurality of hollow fiber membranes 3 and U-shaped middle fiber membranes 3 formed in a U-shape in a microbial reaction tank are fixed, and withdraw the permeate from the hollow fiber membranes 3. A membrane module including an upper end portion and a ring-shaped separator support portion 4 on which a central portion of the U-shaped hollow fiber membrane 3 is hung, and depositing sewage and wastewater to the microbial reactor and using a suction pump. It provides a wastewater treatment method comprising the step of washing the membrane module by discharging the treated water through the outlet (1) of the treated water and supplying the cleaning air through the membrane support (4).

200

/min의 유량으로 공급되는 것이 바람직하다.In the above washing air 1

200

It is preferable to supply at a flow rate of / min.

200

/min의 유량으로 공급되는 것이 바람직하다.The membrane module further includes an internal acid generator 5, and preferably, washing air is supplied through the internal acid generator 5.

200

It is preferable to supply at a flow rate of / min.

[Action]

0.5

, 유효막면적은 1

20㎡/module로서 분리막모듈 상단부(2)에 중공사의 양쪽 끝이 연결되어 있고 정면에서 보면 하부의 분리막 지지부(4)에 가는 U자로 걸린 형태를 보이는 개량형 U형태로 분리막 배분 및 엉킴 방지부(6)에 의해 균일하게 분포된다. 또한 상기한 분리막 세척용 내부 산기장치(5)는 원통형, 사각형 또는 원추형의 형태를 가지며, 고분자, 금속, 세라믹 등의 재질로서 모듈의 중앙에 위치하며 투과공정에서 분리막을 공기로써 세척하는 작용을 한다. 상기 분리막 지지부(4)는 분리막세척용 링 산기장치로서 도넛형태로 위의 분리막세척용 내부산기장치(5)와 함께 분리막을 공기로서 세척한다. 그리고 분리막배분 및 엉킴방지부(6)는 원형의 분리막모듈의 단면을 1-16부분으로 중공사분리막을 배분하고 중공사간의 엉킴을 방지한다.FIG. 1 (a) is a schematic diagram of the deposition type membrane module in which the housing is removed from a general U-shaped hollow fiber membrane module. Figure 1 (b) is immersed in the bioreactor of the drawback of Figure 1 (a) is subjected to filtration tangling prevention of commercial construction of the commercial port is frequent in the present invention to solve the occurrence of floating solid components in the tangled area, etc. As a separator module by the, it is a view showing the portion performing the function of the hollow fiber membrane support in the form of a ring and an air diffuser for cleaning the lower portion of the module. Referring to Figure 1 (b) in more detail, the treated water discharge and back-air inlet (1), the membrane module upper end (2), the internal device for cleaning the membrane (5), hollow fiber membrane (3), membrane support ( 4), the membrane distribution and the entanglement prevention portion (6). Here, the treated water discharge and backwash air inlet 1 is a portion through which the treated water is discharged during the permeation process and the backwash air and water are introduced during the backwash process. The hollow fiber membrane (3) is made of a polymer material such as polysulfone, polyethylene, polypropylene, polyacrylonitrile, and the effective pore size of the membrane is 0.005

0.5

, Effective film area is 1

The membrane distribution and entanglement prevention part is an improved U-shape which shows the shape of U which is connected to both ends of the hollow fiber to the upper part 2 of the separator module as 20 m 2 / module and is viewed from the front of the separator support part 4 in the lower part (6). Evenly distributed by In addition, the separator for cleaning the internal diffuser (5) has a cylindrical, rectangular or conical shape, and is located in the center of the module made of a polymer, metal, ceramic, etc. and serves to clean the separator with air in a permeation process. . The membrane support part 4 is a ring-ring apparatus for washing the membrane, and washes the separator as air together with the above-mentioned internal washing apparatus 5 for washing the membrane in a donut shape. And the membrane distribution and the entanglement prevention portion 6 distributes the hollow fiber membrane to 1-16 parts of the cross-section of the circular membrane module and prevents entanglement between the hollow fibers.

2 (a) is a ring-shaped diffuser, when the U-shaped hollow fiber membrane 3 is supported, the problem of entangled hollow fibers is not completely eliminated. On the contrary, in FIG. 2 (b), the hollow fiber can be moved only in the divided part by dividing the diffuser, thereby preventing the entanglement of the hollow fiber membrane. Integrating these two parts results in a shape similar to that in FIG.

3 is a view showing the fluid flow in the membrane and the membrane module during the permeation and backwashing process. Referring to FIG. 3, the permeated water transmitted from the outer membrane passes through the permeate discharge part 1 through the membrane module upper end part 3 while forming the flow in the direction of the arrow inside the hollow fiber membrane 3. Air introduced through the inlet 1 forms a flow opposite to the permeation process, while penetrating the inside of the hollow fiber membrane 3 to the outside to desorb suspended solids attached to the outer membrane or to form a gel formed on the membrane surface. The layer is removed from the surface.

EXAMPLE

The following presents preferred examples and comparative examples to aid in understanding the invention. However, the following examples are merely provided to more easily understand the present invention, and the present invention is not limited to the following examples.

Example 1

의 반응조 내에 분리막모듈을 침적하고 도시하수를 3

/min의 유량으로 공급하면서 자흡식펌프를 이용하여 (-)100

(-)500mmHg의 압력으로 운전하여 3

/min의 투과수를 얻었다. 상기의 공정은 제4(a)도에 나타내었다.400

The membrane module was deposited in the reactor of

(-) 100 using a self-priming pump while supplying a flow rate of / min

3 by driving with a negative pressure of 500mmHg

Permeate of / min was obtained. The above process is shown in FIG. 4 (a).

, 총질소(total mitrogen: T-N)는 35mg/

및 총인(total phosphorous: T-P)은 5mg/

이었다.The characteristics of the city sewer supplied were as follows. Biochemical Oxygen Demand (BOD) is 100mg /

, Total nitrogen (TN) is 35 mg /

And total phosphorous (TP) is 5 mg /

It was.

Example 2

의 반응조 내에 분리막모듈을 침적하고 도시하수를 3

/min의 유량으로 공급하면서 자흡식펌프를 이용하여 (-)100

(-)500mmHg의 압력으로 운전하여 3

/min의 투과수를 얻었다. 막의 오염을 방지하기 위해 분리막 지지부(4)에서 150

/min의 유량으로 세척공기(a)를 공급하여 운전 중에도 막의 세척이 진행되도록 하였다. 상기의 공정은 제4(b)도에 나타내었다.400

The membrane module was deposited in the reactor of

(-) 100 using a self-priming pump while supplying a flow rate of / min

3 by driving with a negative pressure of 500mmHg

Permeate of / min was obtained. 150 in the membrane support (4) to prevent contamination of the membrane

Washing air (a) was supplied at a flow rate of / min to allow the membrane to be washed even during operation. The above process is shown in FIG. 4 (b).

Example 3

의 반응조 내에 분리막모듈을 침적하고 도시하수를 3

/min의 유량으로 공급하면서 자흡식펌프를 이용하여 (-)100

(-)500mmHg의 압력으로 운전하여 3

/min의 투과수를 얻었다. 막의 오염을 방지하기 위해 분리막 지지부(4)에서 150

/min의 유량으로 세척공기(a)를 공급하여 운전 중에도 막의 세척이 진행되도록 하였고 분리막세척용 내부 산기장치(5)에서 100

/min의 유량으로 세척공기(b)를 공급하여 막의 요동에 의한 분리막세척을 시행하였다. 상기의 공정은 제5(a)도에 나타내었다.400

The membrane module was deposited in the reactor of

(-) 100 using a self-priming pump while supplying a flow rate of / min

3 by driving with a negative pressure of 500mmHg

Permeate of / min was obtained. 150 in the membrane support (4) to prevent contamination of the membrane

The washing air (a) was supplied at a flow rate of / min to allow the membrane to be washed even during operation.

The washing air (b) was supplied at a flow rate of / min to wash the membrane by the shaking of the membrane. The above process is shown in FIG. 5 (a).

Example 4

의 반응조 내에 분리막모듈을 침적하고 도시하수를 3

/min의 유량으로 공급하면서 자흡식펌프를 이용하여 (-)100

(-)500mmHg의 압력으로 운전하여 3

/min의 투과수를 얻었다. 막의 오염을 방지하기 위해 분리막 지지부(4)에서 150

/min의 유량으로 세척공기(a)를 공급하여 운전 중에도 막의 세척이 진행되도록 하였고 분리막세척용 내부 산기장치(5)에서 100

/min의 유량으로 세척공기(b)를 공급하여 막의 요동에 의한 분리막세척을 시행하였다. 1시간의 투과공정후 1분 정도 역세공기 유입부를 통하여 400

700mmHg의 압력, 80

100

/min의 유량으로 공기를 주입하여 역세공정을 실시하고 다시 투과공정을 지속하였다. 상기한 공정을 제5(b)도에 나타내었다.400

The membrane module was deposited in the reactor of

(-) 100 using a self-priming pump while supplying a flow rate of / min

3 by driving with a negative pressure of 500mmHg

Permeate of / min was obtained. 150 in the membrane support (4) to prevent contamination of the membrane

The washing air (a) was supplied at a flow rate of / min to allow the membrane to be washed even during operation.

The washing air (b) was supplied at a flow rate of / min to wash the membrane by the shaking of the membrane. 1 hour after permeation

700mmHg, pressure 80

100

Air was injected at a flow rate of / min to carry out a backwashing process and the permeation process was continued again. The above process is shown in FIG. 5 (b).

의 제거효과를 가져올 수 있으며 폭기조내에 기존 활성슬러지 공정보다 3

5배 이상의 미생물 농도를 유지할 수 있어 폭기조 용량을 1/3

1/5로 축소할 수 있는 효과를 가져올 수 있어 건설비 절감 등의 부가적인 효과도 기대할 수 있다. 또한 막세정을 위한 세정장치를 막모듈 자체에 포함하여 기존의 침지공정의 경우 막오염을 방지하기 위한 교반장치 또는 산기장치의 설치로 인해 장치의 구성이 복잡해지는 문제를 해결할 수 있다.By applying the membrane module of this system to the existing biological treatment process, it is possible to separate solid-liquid with little effect on the properties of microorganisms, so that stable water quality can always be obtained, especially in the case of suspended solids.

It can bring about the removal effect of 3 times than the existing activated sludge process in the aeration tank.

Can maintain microbial concentration 5 times or more

As it can bring down the effect to 1/5, additional effects such as construction cost reduction can be expected. In addition, by including a cleaning device for the membrane cleaning in the membrane module itself, the conventional immersion process can solve the problem of complicated configuration of the device due to the installation of agitator or air diffuser to prevent membrane contamination.

Claims (7)

A plurality of hollow fiber separators formed in a U shape; Both ends of the Middle Eastern separator is fixed and the upper end for withdrawing the permeate from the hollow fiber membrane; A ring-shaped separator support portion on which a central portion of the U-shaped hollow fiber membrane is hung; A membrane distribution and tangle prevention part installed at the membrane support part; And a separator support having a plurality of air supply holes for supplying oxygen or air. The separator module of claim 1, further comprising an internal diffuser device positioned at the center of the separator module to supply air for washing the separator. The effective pore size of the air supply hole is 0.005.

One

And the effective film area is 1

Membrane module of 100㎡ / module. The membrane module of claim 1, wherein the membrane distribution and the entanglement prevention unit have 1 to 16 entanglement prevention protrusions. The separator module of claim 1, wherein the separator module is selected from the group consisting of a cylinder, a rectangle, and a cone. A plurality of hollow fiber separation membranes formed in a U-shape in a microbial reaction tank; Both ends of the hollow fiber membrane is fixed and the upper end for withdrawing the permeate from the hollow fiber membrane; A ring-shaped separation membrane support portion on which a central portion of the U-shaped hollow fiber separation membrane is hung; A membrane distribution and tangle prevention part installed at the membrane support part; The membrane support portion includes a process of depositing a membrane module having a plurality of air supply holes for supplying oxygen or air; Supplying waste water and wastewater to the microbial reactor; Discharging the treated water through an outlet of the treated water using a suction pump; Washing the membrane module by supplying washing air through the membrane support part; Wastewater treatment method comprising a. The wastewater treatment method of claim 6, wherein the separation membrane module further includes an internal air diffuser, and the cleaning air is supplied through the internal air diffuser.

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